Conversion of direct process high-boiling component to chlorosilane monomers in the presence of chlorine

Abstract: The present invention is a process for converting a high-boiling component, resulting from the reaction of an organochloride with silicon, into more commercially desirable monosilanes. The process comprises contacting the high-boiling component with chlorine at a temperature within a range of 250°C. to 1000°C. Improved process yield of monosilanes is obtained by the use of a catalyst selected from alumina, silica, activated carbon, AlCl₃ and AlCl₃ supported on a support selected from alumina, silica and carbon.

Description: The present invention is a process for converting a high-boiling component, resulting from the reaction of an organochloride with silicon, into more commercially desirable monosilanes. The process comprises contacting the high-boiling component with chlorine at a temperature within a range of 250°C. to 1000°C. Improved process yield of monosilanes is obtained by the use of a catalyst selected from alumina, silica, activated carbon, AlCl 3 and AlCl 3 supported on a support selected from alumina, silica and carbon. The high-boiling component useful in our present process results from a process typically referred to as the "Direct Process," where an organohalide is reacted with silicon in the presence of a suitable catalyst to form monosilanes. The Direct Process is described more completely in US-A 2,380,995 and US-A 2,488,487. It is the main commercial process by which organohalosilanes (i.e. monosilanes), for example dimethyldichlorosilane and trimethylchlorosilane, are formed. These organohalosilanes are reactive compounds which can undergo numerous reactions to form a variety of useful silicon containing compounds and polymers. A major commercial use of organohalosilanes is in the production of polysiloxane polymers which are useful as heat transfer fluids, lubricants and the like and which can be further processed, for example, to form silicone elastomers, resins, sealants and adhesives. Operation of the Direct Process results not only in the production of the desirable monosilanes, but also in a high boiling component typically considered to be all materials with a boiling point higher than the particular diorganodihalosilane produced in the process. The high-boiling component is a complex mixture that includes compounds containing SiSi, SiOSi, SiCSi, SiCCSi and SiCCCSi linkages in the molecules. Typical compounds found in a high-boiling component are described in US-A 2,598,435 and US-A 2,681,355. The high-boiling component may also comprise silicon containing solids and soluble and insoluble compounds of copper, aluminum and zinc. In current commercial operations for performing the Direct Process, the high-boiling component can constitute as much as ten percent of the resultant product. Therefore, it is desirable to convert the high-boiling component into commercially desirable products to both reduce low-value by-products and to improve raw materials utilization. The prior art for converting the high boiling component of the Direct Process into more useable monosilanes is represented by US-A 2,598,435, US-A 2,681,355, US-A 2,709,176 and US-A 2,842,580. The present process provides a solution for the problem of conversion of a high-boiling component from the Direct Process to monosilanes. To achieve this solution, our process uses chlorine to facilitate conversion of the high-boiling component. Improved yields of monosilanes can be obtained from our process if a catalyst is used, selected from alumina, silica, activated carbon, AlCl 3 and AlCl 3 supported on a support selected from alumina, silica and carbon, in conjunction with chlorine. The present invention comprises contacting a high-boiling component, resulting from the reaction of an organochloride with silicon and chlorine gas at a temperature within a range of 250°C. to 1000°C. Improved yield of monosilanes in the process is obtained by the use of a catalyst selected from alumina, silica, activated carbon, AlCl 3 and AlCl 3 supported on a support selected from alumina, silica and carbon. The present process may be run in any standard type reactor for contacting silanes and chlorine. The process may be run as a batch process, semi-continuous or continuous process. The process can be run, for example, in a fixed-bed reactor, a stirred-bed reactor or a fluidized-bed reactor. Preferred is when the process is run as a continuous process in a fluidized-bed reactor. The present process is useful for converting a high-boiling component resulting from the reaction of an organochloride with silicon to form monosilanes. The term "high-boiling component" refers to those materials with a boiling point above that of the diorganodichlorosilane formed by the reaction of the organochloride with silicon. For example when methyl chloride is reacted with silicon, the diorganodichlorosilane will be dimethyldichlorosilane and the high-boiling component will comprise those materials having a boiling point greater than that of dimethyldichlorosilane, i.e. greater than 70°C. In a typical process for reacting an organo-chloride with silicon, the reaction is conducted at a temperature of 270°C. to 350°C., in the presence of a suitable catalyst, gaseous product and unreacted feed are continuously removed from the process. The removed gaseous product and unreacted feed are subsequently distilled to remove monosilanes leaving behind a high-boiling component. The high-boiling component is a complex mixture that includes compounds containing SiSi, SiOSi, SiCSi, SiCCSi and SiCCCSi linkages alone or in combination in each molecule. The high-boiling component can include silicon containing solids and soluble and insoluble compounds of copper, aluminum and zinc. The high-boiling component may contain, for example, organic substituted and non-organic substituted silanes, disilanes, trisilanes, disiloxanes, silane oligomers, siloxane oligomers, silalkylenes and silicon containing solids, all of which may be converted to monosilanes by our process. The present process is especially useful for converting polysilanes in the high-boiling component to monosilanes, where the polysilanes are described by formula R a H b Si n Cl 2n+2-a-b and where each R is a radical independently selected from alkyls comprising one to six carbon atoms, n=2 to 20, a=0 to 2n+2, b=0 to 2n+2 and a+b=0 to 2n+2. The polysilanes useful in the present process can consist of n number of silicon atoms where n is an integer from two to 20. Preferred is when n equals two. The polysilanes can be substituted with a=0 to 2n+2 number of R radicals, where each R is independently selected from alkyls of one to six carbon atoms. The radical R can be methyl, ethyl, propyl and t-butyl. Preferred is when R is methyl. The polysilanes in the high-boiling component can contain b number of hydrogen atoms substituted on the silicon atoms, where b=0 to 2n+2. The polysilanes in the high-boiling component can also contain from zero to 2n+2 chlorine atoms. The high-boiling component can contain silalkylenes, where each silalkylene can comprise one or more silalkylene bonds described by formula Si(C) z Si and z is an integer from one to six. Preferred is when z is an integer from one to three. The silalkylene molecules can comprise SiSi bonds and SiOSi bonds as well as silalkylene bonds. The silicon atoms of the silalkylene molecules can be further substituted with the radical R, where R is as previously described, with chlorine and with hydrogen. Preferred is when the silicon atoms of the silalkylenes are substituted with methyl. The preferred high-boiling component is one resulting from the reaction of methyl chloride with silicon, the high-boiling component having a boiling point greater than 70°C. The high-boiling component can contain Me 2 ClSiSiMe 2 Cl, Me 2 ClSiSiMeCl 2 , MeCl 2 SiSiMeCl 2 , Me 2 ClSiSi(Me)(Cl)SiMeCl 2 , Me 2 ClSiCH 2 SiMe 2 Cl, Me 2 ClSiCH 2 SiMeCl 2 , MeCl 2 SiCH 2 SiMeCl 2 , MeClSi(CH 2 ) 2 SiMeCl 2 , Me 2 ClSi(CH 2 ) 3 SiMeCl 2 , Me 2 ClSiCH 2 Si(Me)(Cl)SiMeCl 2 , Me 2 ClSiCH 2 Si(Me)(Cl)CH 2 SiMeCl 2 and Me 2 ClSiOSiMeCl 2 , where Me is methyl, all of which may be converted to monosilanes by the present process. The high-boiling component is contacted with chlorine provided to the reactor as a gas, where the ratio of the weight of high-boiling component to the weight of chlorine added to the reactor is within a range of 10:1 to 0.05:1. Preferred is where the ratio of the weight of high-boiling component to the weight of chlorine is within a range of 3:1 to 1:1. The process is conducted at a temperature within a range of 250°C. to 1000°C. A preferred temperature is within a range of 270°C. to 650°C. While pressure is not critical to the present process, it is preferred that the process be run at a gauge pressure within a range of 0 to 6.9 MPa (zero to 1000 psi). The present process can be conducted in the presence of a catalyst selected from alumina, silica, activated carbon, AlCl 3 and AlCl 3 supported on a support selected from alumina, silica and carbon. The physical form of the catalyst is not critical to the present invention and can be, for example, powder particles, flakes, chips and pellets. The amount of catalyst required in the process will depend on such factors as the reactor type employed, the specific catalyst used, the chemical composition of the high-boiling component and the process temperature. When the process is run as a batch process or a semi-continuous process a useful weight of catalyst is within a range of 0.1 to 30 weight percent of the combined weight of the high boiling component and the chlorine added to the process. The catalyst can be alumina, i.e. Al 2 O 3 . The size of the alumina is not critical to the present process and is determined by commercial availability and the ability to be handled. Generally alumina with a particle size within a range of 0.001 mm to 10 mm is considered useful. The catalyst can be silica and can be selected from precipitated silica, fumed silica or silica gel. Generally, silica with a particle size within a range of 0.001 mm to 10 mm is useful. The catalyst can be activated carbon. By "activated carbon", it is meant a microcrystalline, nongraphite form of carbon, having an internal porosity, the carbon having been activated by any standard process known in the art for producing activated carbon, such as chemical activation or gas activation, as described in Kirk-Othmer, Concise Encyclopedia of Chemical Technology, John Wiley & Sons publishers, 1985, p. 204 to 205. In general, it is preferred that the activated carbon have a diameter within a range of 0.001 mm to 20 mm. More preferred is when the activated carbon has a diameter within a range of 0.01 mm to 5 mm and a surface area greater than 1000 m 2 /g. The catalyst can be AlCl 3 retained on a support selected from alumina, silica and carbon. The amount of AlCl 3 supported on the support can be from 0.1 to 20 weight percent AlCl 3 . Preferred is when the amount of AlCl 3 is within a range of 0.5 to 5.0 weight percent. The concentration of unsupported AlCl 3 useful in the present process is similar to that described above. The optimum contact time for the high-boiling component and chlorine with the catalyst will depend on factors such as the type of catalyst, chemical composition of the high-boiling component and the degree of conversion and product selectivity desired. In general, a contact time within a range of one second to five hours is considered useful. A longer contact time may be employed, but appears to offer no advantage and could result in excessive scission of silicon-carbon bonds and silicon-hydrogen bonds in the monosilanes. A preferred contact time in a continuous reactor system is within a range of one second to one hour. If desired, the monosilane containing product of our process can be further separated by standard means, for example, distillation to separate the monosilanes from a high-boiling component with the high-boiling component subsequently recycled to the process. The following examples are provided to facilitate understanding and to demonstrate the effectiveness of the present invention. Example 1 (Not within the scope of the present invention). A high-boiling component resulting from the reaction of methyl chloride with silicon was contacted with hydrogen chloride in the absence of catalyst. The reactor consisted of a 2.5 cm diameter by 50 cm length quartz tube maintained at 500°C. The high-boiling component comprised by weight, 55% methylchlorodisilane, 5% disilmethylenes, 35% polysilanes and silalkylenes and 5% silicon containing solids. The high-boiling component was fed at a rate of 117 g/h to the reactor and hydrogen chloride was fed to the reactor at 50 g/h. The process was conducted for one hour with gaseous products exiting the reactor being collected in a cold condenser. The condensed product was analyzed by gas chromatography using a thermal conductivity detector (GC-TC) and found to consist of 59 weight percent chlorosilane monomers. Chlorosilane monomers detected included HSiCl 3 , SiCl 4 , MeHSiCl 2 , Me 3 SiCl, MeSiCl 3 and Me 2 SiCl 2 . Other species detected in the condensed product included methylchlorodisilanes, disilmethylenes, polysilanes and silalkylenes. Example 2 A high-boiling component resulting from the reaction of methyl chloride with silicon was contacted with chlorine in the absence of a catalyst. The process was conducted similar to that described in Example 1, with the high-boiling component composition, reactor design and reaction temperature being the same. The run was conducted for ten to 15 minutes. The high-boiling component was fed to the reactor at a rate of 147 g/h and chlorine gas was fed to the reactor at a rate of 86 g/h. Gaseous product exiting the reactor was collected and analyzed as described in Example 1. The collected product was found to comprise 72 weight percent chlorosilane monomers and included those chlorosilane monomers described for the product of Example 1. Example 3 A high-boiling component resulting from the reaction of methyl chloride with silicon was contacted with chlorine in the presence of activated carbon catalyst in a fluidized-bed reactor. The composition of the high-boiling component and reactor design was similar to that described in Example 1. The process was conducted at a temperature of 400°C. The reactor was filled with 20 g of a 0.1 mm to 0.3 mm pulverized activated carbon (North American, Columbus, OH). The high-boiling component was fed to the reactor at a rate of 158 g/h and chlorine gas was fed to the reactor at a rate of 135 g/h. The process was conducted for ten to 15 minutes with the gaseous product exiting the reactor being collected and analyzed as described in Example 1. The collected product was determined to consist of similar species as identified in Example 1. Of the product collected, 87 weight percent was chlorosilane monomers.

Claims: A process for converting a high-boiling component, resulting from the reaction of an organochloride with silicon, to monosilanes, the process comprising contacting the high-boiling component with chlorine gas at a temperature within a range of 250°C. to 1000°C. A process according to claim 1 where the process is conducted at a gauge pressure within a range of 0 to 6.9 MPa (zero to 1,000 psi). A process according to claim 1 where the ratio of the weight of the high-boiling component to the weight of the chlorine is within a range of 10:1 to 0.05:1. A process according to claim 1 where the high-boiling component results from the reaction of methyl chloride with silicon and the high-boiling component comprises polysilanes, silalkylenes, silicon containing solids and soluble and insoluble compounds of copper, aluminum and zinc. A process according to claim 1 where the high-boiling component comprises polysilanes described by formula R a H b Si n Cl 2n+2-a-b , where each R is a radical independently selected from alkyls comprising one to six carbon atoms, n=2 to 20, a=0 to 2n+2, b=0 to 2n+2 and a+b=0 to 2n+2. A process according to claim 1 where the high-boiling component comprises silalkylenes which comprise one or more silalkylene bonds and are described by formula Si(C) z Si and z=1, 2 or 3. The process of claim 1 wherein the process is conducted in the presence of a catalyst selected from alumina, silica, activated carbon, AlCl 3 and AlCl 3 supported on a support selected from alumina, silica and carbon. A process according to claim 7 where the process is run as a batch or semi-continuous process and concentration of the catalyst is within a range of 0.1 to 30 weight percent of the combined weight of the high-boiling component and the chlorine added to the process. A process according to claim 7 where the catalyst is activated carbon having a diameter within a range of 0.01 mm to 5 mm and a surface area greater than 1000 m 2 /g.

Inventors: CHADWICK KIRK MICHAEL, DHAUL AJAY KUMAR, HALM ROLAND LEE, JOHNSON RICHARD GORDON, STEINMEYER ROBERT DAVID, CHADWICK, KIRK MICHAEL, DHAUL, AJAY KUMAR, HALM, ROLAND LEE, JOHNSON, RICHARD GORDON, STEINMEYER, ROBERT DAVID
Applicants: DOW CORNING, DOW CORNING CORPORATION
Application year: 1994
Main classification: C07F7
IPC codes: C07F7, C01B33